U.S. patent application number 16/618751 was filed with the patent office on 2021-01-07 for catalyst, and method for direct conversion of syngas to prepare light olefins.
The applicant listed for this patent is DALIAN INSTITUTE OF CHEMICAL PHYSICS, CHINESE ACADEMY OF SCIENCES. Invention is credited to Xinhe BAO, Feng JIAO, Xiulian PAN.
Application Number | 20210002184 16/618751 |
Document ID | / |
Family ID | |
Filed Date | 2021-01-07 |
United States Patent
Application |
20210002184 |
Kind Code |
A1 |
PAN; Xiulian ; et
al. |
January 7, 2021 |
CATALYST, AND METHOD FOR DIRECT CONVERSION OF SYNGAS TO PREPARE
LIGHT OLEFINS
Abstract
A process for direct synthesis of light olefins uses syngas as
the feed raw material. This catalytic conversion process is
conducted in a fixed bed or a moving bed using a composite catalyst
containing components A and B (A+B). The active ingredient of
catalyst A is metal oxide; and catalyst B is an oxide supported
zeolite. A carrier is one or more of Al.sub.2O.sub.3, SiO.sub.2,
TiO.sub.2, ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3 having
hierarchical pores; the zeolite is one or more of CHA and AEI
structures. The loading of the zeolite is 4%-45% wt. A weight ratio
of the active ingredients in the catalyst A and the catalyst B is
within a range of 0.1-20, and preferably 0.3-5. The total
selectivity of the light olefins comprising ethylene, propylene and
butylene can reach 50-90%, while the selectivity of a methane
byproduct is less than 15%.
Inventors: |
PAN; Xiulian; (Dalian,
Liaoning, CN) ; JIAO; Feng; (Dalian, Liaoning,
CN) ; BAO; Xinhe; (Dalian, Liaoning, CN) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
DALIAN INSTITUTE OF CHEMICAL PHYSICS, CHINESE ACADEMY OF
SCIENCES |
Dalian, Liaoning |
|
CN |
|
|
Appl. No.: |
16/618751 |
Filed: |
August 2, 2018 |
PCT Filed: |
August 2, 2018 |
PCT NO: |
PCT/CN2018/098379 |
371 Date: |
February 25, 2020 |
Current U.S.
Class: |
1/1 |
International
Class: |
C07C 1/04 20060101
C07C001/04; B01J 21/04 20060101 B01J021/04; B01J 21/06 20060101
B01J021/06; B01J 23/00 20060101 B01J023/00; B01J 23/06 20060101
B01J023/06; B01J 23/10 20060101 B01J023/10; B01J 23/26 20060101
B01J023/26; B01J 23/34 20060101 B01J023/34; B01J 29/70 20060101
B01J029/70; B01J 21/08 20060101 B01J021/08; B01J 29/85 20060101
B01J029/85 |
Foreign Application Data
Date |
Code |
Application Number |
Jun 2, 2017 |
CN |
201710408018.9 |
Claims
1. A catalyst, wherein the catalyst is a composite catalyst
composed of A+B; the catalyst component A and the catalyst
component B are compounded by mechanical mixing method; the active
ingredients of the catalyst component A are active metal oxides;
the catalyst component B are supported zeolites; the carrier is at
least one of porous Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2,
ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3; the zeolite is at
least one of CHA and AEI structures; the loading of the zeolite is
4%-45% wt; and the active metal oxide is at least one of MnO,
MnCr.sub.2O.sub.4, MnAl.sub.2O.sub.4, MnZrO.sub.4, ZnO,
ZnCr.sub.2O.sub.4, ZnAl.sub.2O.sub.4, CoAl.sub.2O.sub.4 and
FeAl.sub.2O.sub.4.
2. The catalyst according to claim 1, wherein at least one of
porous Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2, ZrO.sub.2, CeO.sub.2,
MgO and Ga.sub.2O.sub.3 in the catalyst component B is used as the
carrier; specific surface area is 30-250 m.sup.2/g; pore volume is
0.25-0.80 ml/g; through calculation according to the specific
surface area, mesoporous specific surface area occupies 30-75% and
macroporous specific surface area occupies 25-70%; and the zeolite
is used as an active component and dispersed on the carrier by in
situ growth or physical mixing mode.
3. The catalyst according to claim 1, wherein component A is at
least one of MnO, MnCr.sub.2O.sub.4, MnAl.sub.2O.sub.4,
MnZrO.sub.4, ZnAl.sub.2O.sub.4, CoAl.sub.2O.sub.4 and
FeAl.sub.2O.sub.4.
4. The catalyst according to claim 1, wherein a weight ratio
between the active ingredient in the catalyst component A and the
catalyst component B is within the range of 0.1-20.
5. The catalyst according to claim 1, wherein the active metal
oxide is composed of crystals with a size of 5-30 nm, and a large
amount of oxygen vacancies exist within a distance range of 0.3 nm
from the surfaces of the crystals to the internal direction of the
crystals, wherein the molar weight of oxygen atoms occupies a value
less than 80% of the oxygen molar content in theoretical
stoichiometric ratio.
6. The catalyst according to claim 1, wherein a dispersing agent is
also added to the catalyst A; the dispersing agent is at least one
of Al.sub.2O.sub.3, SiO.sub.2, Cr.sub.2O.sub.3, ZrO.sub.2 and
TiO.sub.2; the active metal oxide is dispersed on the dispersing
agent; and the content of the dispersing agent in the catalyst A is
0.05-90 wt %, and the balance is the active metal oxide.
7. A method for synthesis of light olefins directly from syngas,
wherein syngas is used as raw material; the conversion process is
conducted on a fixed bed or a moving bed; and the adopted catalyst
is the catalyst of claim 1; tpressure of the syngas is 0.5-10 MPa;
reaction temperature is 300-600.degree. C.; space velocity is
300-10000 h.sup.-1; and the ratio of syngas H.sub.2/CO for reaction
is 0.2-3.5.
8. The catalyst according to claim 4, wherein the weight ratio
between the active ingredient in the catalyst component A and the
catalyst component B is within the range of 0.3-5.
9. The catalyst according to claim 5, wherein the molar weight of
oxygen atoms occupies a value of 10%-80% of the oxygen molar
content in theoretical stoichiometric ratio.
10. The catalyst according to claim 5, wherein a surface oxygen
vacancy concentration is 20-90%, wherein surface oxygen vacancy is
a percentage of the molar weight of oxygen atoms over a
stoichiometric molar weight of oxygen; and corresponding more
preferably 40-90% and most preferably 50-90%.
11. The catalyst according to claim 10, wherein the surface oxygen
vacancy concentration is 40-90%.
12. The catalyst according to claim 11, wherein the surface oxygen
vacancy concentration is 50-90%.
Description
TECHNICAL FIELD
[0001] The present invention belongs to synthesis of light olefins
using syngas, and particularly relates to a catalyst and a method
for synthesizing light olefins via direct conversion of syngas.
BACKGROUND
[0002] Light olefins refer to alkenes with the number of carbon
atoms less than or equal to 4. Light olefins, including ethylene,
propylene and butene, are very important basic organic chemical raw
materials. With the fast growth of economy in China, the market of
the light olefins is in short supply for a long time. At present,
the light olefins are produced mainly through a petrochemical route
of cracking of light hydrocarbon (ethane, naphtha and light diesel
fuel). Due to the increasing shortage of global petroleum resources
and the long-term high-price operation of crude oil, the
development of the light olefin industry relying only on a tubular
cracking furnace technology that uses petroleum light hydrocarbon
as raw material will encounter more and more difficulties in raw
material. The production technology and the raw material of the
light olefins must be diversified. A technology for preparing
alkene using syngas can widen the source of the raw material, and
will provide an alternative solution for a steam cracking
technology based on high-cost raw material such as naphtha by
production of syngas using crude oil, natural gas, coal and
renewable material as raw material. One-step direct preparation of
the light olefins using the syngas is a process of directly
preparing the light olefins with the number of carbon atoms less
than or equal to 4 through Fischer-Tropsch synthesis reaction of
carbon monoxide and hydrogen under the action of the catalyst. This
process simplifies the process flow and greatly reduces the
investment unlike an indirect method that further prepares the
alkene from the syngas and the methanol or dimethyl ether.
[0003] Direct preparation of the light olefins using the syngas
through Fischer-Tropsch synthesis has become one of research
hotspots in development of catalyst for Fischer-Tropsch synthesis.
In patent CN1083415A disclosed by Dalian Institute of Chemical
Physics, Chinese Academy of Sciences, high activity (CO conversion
rate: 90%) and selectivity (light olefins selectivity: 66%) can be
obtained under reaction pressure of 1.0 to 5.0 MPa and reaction
temperature of 300 to 400.degree. C. in preparation of the light
olefins from the syngas under the auxiliary of alkali K or Cs ion
by using an iron-manganese catalyst system carried by IIA alkali
metal oxide such as MgO or silica rich zeolite (or
phosphorous-aluminum zeolite). In patent ZL03109585.2 declared by
Beijing University of Chemical Technology, Fe/activated carbon
catalyst with manganese, copper, zinc, silicon and potassium as
auxiliaries is prepared by a vacuum impregnation method for the
reaction of preparation of the light olefins from the syngas. Under
the condition of no feedstock gas circulation, the CO conversion
rate is 96%, and the selectivity of the light olefins in
hydrocarbons is 68%. In 2012, professor de Jong's team at Utrecht
university in Netherlands made good progress by using Fe catalyst
modified by Fe, Na, S and other auxiliaries supported by SiC,
carbon nanofiber and other inert carriers, obtained 61% of
selectivity of light olefins. However, the selectivity is reduced
when the conversion rate is increased. In 2016, researcher Sun
Yuhan and researcher Zhong Liangshu in Shanghai Advanced Research
Institute reported a preferred exposure [101] and [020]
manganese-assisted cobalt carbide based catalyst, and realized
60.8% of selectivity of light olefins and 5% of selectivity of
methane at a CO conversion rate of 31.8%. In the above report, the
catalyst uses an iron or cobalt based catalyst as an active
component. The reaction follows the chain growth reaction mechanism
of metal surfaces. The selectivity of the product light olefins is
low.
[0004] Recently, a composite bifunctional catalyst of
ZnCr.sub.2O.sub.4 oxide and hierarchical pore SAPO-34 zeolite has
been reported by academician Bao Xinhe and professor Pan Xiulian in
Dalian Institute of Chemical Physics, Chinese Academy of Sciences
(Jiao et al., Science 351 (2016) 1065-1068), which has realized 80%
of selectivity of the light olefins when the conversion rate of CO
is 17%, wherein the selectivity of the light olefins is 14 and the
alkene/alkane ratio is 5.7. When the conversion rate is increased
to 35%, the alkene selectivity is 69%, alkane selectivity is 20%,
and the alkene/alkane ratio is decreased to 3.5. How to achieve
high conversion rate while stabilizing the alkene/alkane ratio is
still a major difficulty in the field.
SUMMARY OF INVENTION
[0005] In view of the above problems, the present invention
provides a catalyst and a method for preparing light olefins using
direct conversion of syngas. The technical solution of the present
invention is as follows:
[0006] A catalyst, characterized in that the catalyst is a
composite catalyst A+B; the catalyst component A and the catalyst
component B are compounded by mechanical mixing method; the active
ingredient of the catalyst component A is an active metal oxide;
catalyst B is one or more of zeolite of CHA and AEI structures with
a carrier of one or more of Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2,
ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3 having hierarchical
pores; the loading of the zeolite in B is 4%-45% wt;
[0007] and the active metal oxide is one or more than one of MnO,
MnCr.sub.2O.sub.4, MnAl.sub.2O.sub.4, MnZrO.sub.4, ZnO,
ZnCr.sub.2O.sub.4, ZnAl.sub.2O.sub.4, CoAl.sub.2O.sub.4 and
FeAl.sub.2O.sub.4.
[0008] The catalyst characterized in that one or more of
hierarchical pores Al.sub.2O.sub.3, SiO.sub.2, TiO.sub.2,
ZrO.sub.2, CeO.sub.2, MgO and Ga.sub.2O.sub.3 in the catalyst
component B is used as the carrier; specific surface area is 30-250
m.sup.2/g; pore volume is 0.25-0.80 ml/g; through calculation
according to the specific surface area, mesoporous specific surface
area occupies 30-75% and macroporous specific surface area occupies
25-70%; and the zeolite is used as an active component and
dispersed around the carrier by in situ growth or physical mixing
mode.
[0009] The catalyst characterized in that component A is preferably
one or more than one of MnO, MnCr.sub.2O.sub.4, MnAl.sub.2O.sub.4,
MnZrO.sub.4, ZnAl.sub.2O.sub.4, CoAl.sub.2O.sub.4 and
FeAl.sub.2O.sub.4.
[0010] The catalyst characterized in that a spacing between
geometric centers of the active metal oxide of the catalyst
component A and the particle of the component B is 50 nm-20 mm,
preferably 300 nm-5 mm and more preferably 1 .mu.m-2.5 mm.
[0011] The catalyst characterized in that a weight ratio between
the active ingredient in the catalyst component A and the catalyst
component B is within the range of 0.1-20, and preferably
0.3-5.
[0012] The catalyst characterized in that the active metal oxide is
composed of crystals with a size of 5-30 nm, and a large amount of
oxygen vacancies exist within a distance range of 0.3 nm from the
surfaces of the crystals to the internal direction of the crystals,
wherein the molar weight of oxygen atoms occupies a value less than
80% of the oxygen molar content in theoretical stoichiometric
ratio, preferably, 80%-10%, more preferably 60%-10% and most
preferably 50%-10%; the surface oxygen vacancies are defined as:
100%-percent of the molar weight of oxygen atoms in theoretical
stoichiometric ratio of oxygen molar weight; and corresponding
oxygen vacancy concentration is preferably 20-90%, more preferably
40-90% and most preferably 50-90%.
[0013] The catalyst characterized in that a dispersing agent is
also added to the catalyst A; the dispersing agent is one or more
than one of Al.sub.2O.sub.3, SiO.sub.2, Cr.sub.2O.sub.3, ZrO.sub.2
and TiO.sub.2; the active metal oxide is dispersed in the
dispersing agent; and the content of the dispersing agent in the
catalyst A is 0.05-90 wt %, and the balance is the active metal
oxide.
[0014] A method for preparing light olefins using direct conversion
of syngas, characterized in that syngas is used as reaction raw
material; a conversion reaction is conducted on a fixed bed or a
moving bed; and the adopted catalyst is the catalyst of any one of
claims 1-7; the pressure of the syngas is 0.5-10 MPa; reaction
temperature is 300-600.degree. C.; space velocity is
300-10000h.sup.-1; and the ratio of syngas H.sub.2/CO for reaction
is 0.2-3.5.
[0015] The dual-function composite catalyst is used for preparing
light olefins using one-step direct conversion of syngas, wherein
the sum of the selectivity of ethylene and propylene reaches
40-60%; the sum of the selectivity of the light olefins comprising
ethylene, propylene and butylene can reach 50-90%, while the
selectivity of a methane byproduct is less than 15%.
[0016] The present invention has the following advantages:
[0017] 1. Different from the traditional technology for preparing
the light olefins through methanol (MTO for short), this technology
realizes preparation of the light olefins through one-step direct
conversion of syngas.
[0018] 2. Because of the hierarchical pore carrier dispersed
zeolite, it is beneficial to the mass transfer of the intermediate
and the product, thereby greatly reducing the influence of side
reactions such as hydrogenation and maintaining high selectivity of
the light olefins while increasing the conversion rate.
[0019] 3. The composite catalyst in the patent is simple in
preparation process and mild in conditions. The reaction process
has an extremely high product yield and selectivity, with the
selectivity for C.sub.2-C.sub.4 light olefins reaching 50-90% and
especially can still maintain high alkene/alkane ratio after
increasing the conversion rate. Meanwhile, the selectivity of the
methane byproduct is low (<15%), and the catalyst has long
service life which is longer than 700 hours. The present invention
has excellent application prospect.
DETAILED DESCRIPTION
[0020] The present invention is further illustrated below by
embodiments, but the scope of claims of the present invention is
not limited by the embodiments. Meanwhile, the embodiments only
give some conditions for achieving the purpose, but it doesn't mean
that the conditions must be satisfied to achieve the purpose.
Embodiment 1
[0021] I. Preparation of catalyst A
[0022] (I) Synthesizing ZnO Material with Polar Surface Through an
Etching Method Comprises:
[0023] (1) respectively weighing 4 parts of 0.446 g (1.5 mmol) of
Zn(NO.sub.3).sub.2.6H.sub.2O into four containers; respectively
weighing 0.300 g (7.5 mmol), 0.480 g (12 mmol), 0.720 g (18 mmol)
and 1.200 g (30 mmol) of NaOH and successively adding to the above
four container; weighing 30 ml of deionized water and adding to the
four containers; stirring for a time greater than 0.5 h to
uniformly mix a solution; increasing the temperature to 160.degree.
C. with the reaction time of 20 h; decomposing precipitate into
zinc oxide; naturally cooling to room temperature; centrifugally
separating reaction liquid to collect the centrifugally separated
precipitate; and washing with deionized water twice to obtain ZnO
oxide;
[0024] taking a product with 0.480 g (12 mmol) of NaOH for the
following processing:
[0025] (2) ultrasonically mixing an etching agent, such as oleic
acid, hexamethylenetetramine, ethylenediamine, ammonia and
hydrazine hydrate, with ZnO oxide uniformly under normal
temperature; immersing the ZnO oxide in the solution of the etching
agent; and generating a complexing or direct reduction reaction by
the etching agent and the zinc oxide;
[0026] heating the above suspended matter; then taking out the
suspended matter for washing and filtering the suspended matter to
obtain active nano ZnO material having a large amount of surface
oxygen holes.
[0027] In Table 1: the mass ratio of the catalyst to the etching
agent is 1:3. The mass ratio of the oleic acid to the
hexamethylenetetramine is 1:1, without solvent. The mass ratio of
the oleic acid (5 wt %) to the hydrazine hydrate is 95:5, without
solvent. Specific treatment conditions include the etching agent,
temperature, treatment time and atmosphere types as shown in Table
1 below.
[0028] (3) Drying or Drying and Reducing:
[0029] after centrifuging or filtering the above obtained products
and washing the products with deionized water, drying or drying and
restoring the products in an atmosphere which is inert gas or a gas
mixture of inert gas and a reducing atmosphere, wherein the inert
gas is one or more than one of N.sub.2, He and Ar, the reducing
atmosphere is one or more than one of H.sub.2 and CO; a volume
ratio of the inert gas to the reducing gas in the dried and
restored gas mixture is 100/10-0/100, the temperature of drying and
restoring is 350.degree. C., and time is 4 h. ZnO material with
abundant oxygen vacancies on the surface is obtained. Specific
samples and preparation conditions thereof are shown in Table 1
below. The surface oxygen vacancies are defined as: (1-percent of
the molar weight of oxygen atoms in theoretical stoichiometric
ratio of oxygen molar content).
TABLE-US-00001 TABLE 1 Preparation of ZnO Material and Parameter
Performance Temperature/.degree. C. Drying or Drying and Surface
Sample and carrier gas Ti Reducing Temperature/.degree. C. Oxygen
Number Etching Agent (V/V) (Minute) and Atmosphere Vacancy ZnO 1
oleic acid- 100, N.sub.2 30 30, N.sub.2 21% hexamethylene tetramine
ZnO 2 oleic acid 100, 5% H.sub.2/N.sub.2 30 300, 5% H.sub.2/N.sub.2
45% ZnO 3 oleic acid 120, 5% CO/Ar 60 350, 5% CO/Ar 67% ZnO 4 oleic
acid-5 wt % 140, 5% H.sub.2/Ar 60 310, 5% H.sub.2/Ar 73% hydrazine
hydrate ZnO 5 ethylenediamine 100, 5% NH.sub.3/Ar 30 250, 5%
NH.sub.3/Ar 30% ZnO 6 ethylenediamine 140, 5% NO/Ar 90 150, 5%
NO/Ar 52% ZnO 7 20 wt % 100, Ar 30 120, 5% CO/Ar 22% ammonium
hydroxide ZnO 8 20 wt % 140, 5% NH.sub.3/5% NO/Ar 90 400, He 29%
ammonium hydroxide
[0030] The surface oxygen vacancies are the percent of the molar
weight of oxygen atoms in theoretical stoichiometric ratio of
oxygen molar content within a distance range of depth 0.3 nm from
the surfaces of the crystals to the internal direction of the
crystals.
[0031] As a reference example, the surface which is not etched in
step (2) has no oxygen vacancy ZnO 9, and metal Zn 10 that
completely reduces Zn.
[0032] (II) Synthesizing MnO material with polar surface through an
etching method: the preparation process is the same as described in
(I) (1) for the product with 0.480 g (12 mmol) of NaOH and (3). The
difference is that, the precursor of Zn is changed for the
corresponding precursor of Mn, which may be one of manganous
nitrate, manganese chloride and manganese acetate, and is manganous
nitrate herein.
[0033] The etching process is the same as the preparation processes
of products ZnO 3, ZnO 5 and ZnO 8 in step (2) in above (I). The
catalyst having a great number of surface oxygen vacancies is
synthesized. The surface oxygen vacancies are 67%, 29% and 27%.
[0034] Corresponding products are defined as MnO 1-3.
[0035] (III) Synthesizing CeO.sub.2 material with polar surface
through an etching method: the preparation process is the same as
that of the above (I)(1) for the product with 0.480 g (12 mmol) of
NaOH and (3). The difference is that, the precursor of Zn is
changed for the corresponding precursor of Ce, which may be one of
cerium nitrate, cerium chloride and cerous acetate and is cerium
nitrate herein.
[0036] The etching process is the same as the preparation processes
of products ZnO 3, ZnO 5 and ZnO 8 in step (2) in above (I). The
catalyst having a great number of surface oxygen vacancies is
synthesized. The surface oxygen vacancies are 56%, 33% and 21%.
[0037] Corresponding products are defined as CeO 1-3.
[0038] (IV) Synthesizing nano ZnCr.sub.2O.sub.4, ZnAl.sub.2O.sub.4,
MnCr.sub.2O.sub.4, MnAl.sub.2O.sub.4 and MnZrO.sub.4 spinel with
high specific surface area and high surface energy comprises:
[0039] adopting zinc nitrate, aluminum nitrate, chromic nitrate,
manganous nitrate and zirconium nitrate as precursors, and mixing
with urea at room temperature in water; aging the above mixed
liquid; then taking out the mixed liquid for washing, filtering and
drying the mixed liquid; and roasting the obtained solid under an
air atmosphere to obtain spinel oxide which grows along the (110)
crystal plane direction. The sample is also treated by the etching
method to synthesize the catalyst with a great number of surface
oxygen vacancies. The etching process and aftertreatment process
are the same as step (2) and step (3) in above (I). The sample has
large specific surface area and many surface defects, and can be
applied to catalyzing the conversion of syngas.
[0040] Specific samples and preparation conditions thereof are
shown in Table 2 below. Similarly, the surface oxygen vacancies are
defined as: (1-percent of the molar weight of oxygen atoms in
theoretical stoichiometric ratio of oxygen molar content).
TABLE-US-00002 TABLE 2 Preparation of Spinel Material and
Performance Parameters Stoichiometric Ratio of Metal Elements in
Etching Agent, Spinel and Final Molar Aging Roasting
Temperature/.degree. C., Surface Sample Concentration of Metal
Temperature .degree. C. Temperature .degree. C. Atmosphere and
Oxygen Number in Water (mmol/L) and Time h and Time h Time/min
Vacancy spinel 1 ZnCr = 1:2, 120, 24 600, 48 oleic acid, 120, 41%
Zn is 50 mM 5% H.sub.2/Ar, 60 spinel 2 ZnAl = 1:2, 130, 20 700, 24
oleic acid, 120, 72% Zn is 50 mM 5% H.sub.2/Ar, 60 spinel 3 MnCr =
1:2, 140, 18 750, 16 oleic acid, 120, 83% Mn is 50 mM 5%
H.sub.2/Ar, 60 spinel 4 MnAl = 1:2, 145, 16 800, 10 oleic acid,
120, 20% Mn is 50 mM 5% H.sub.2/Ar, 60 spinel 5 MnZr = 1:2, 150, 12
900, 3 oleic acid, 120, 24% Mn is 50 mM 5% H.sub.2/Ar, 60
[0041] (V) Synthesizing nano FeAl.sub.2O.sub.4, CoAl.sub.2O.sub.4
and spinel with high specific surface area and high surface energy:
the preparation process is the same as (2) of the above (IV). The
difference is that, the precursor of Zn is changed for the
corresponding precursor of Fe or Co, which is one of ferric
nitrate, ferric chloride and ferric citrate or one of cobalt
nitrate, cobalt chloride and cobalt acetate and is ferric nitrate
and cobalt nitrate herein.
[0042] etching process is the same as the preparation processes of
products ZnO 3 and ZnO 5 in step (2) in above (I). The catalyst
having a great number of surface oxygen vacancies is synthesized.
The surface oxygen vacancies are 77% and 51%.
[0043] Corresponding products are defined as spinel 6 and spinel
7.
[0044] (VI) Cr.sub.2O.sub.3, Al.sub.2O.sub.3 or ZrO.sub.2 dispersed
active metal oxide
[0045] Cr.sub.2O.sub.3, A.sub.2O.sub.3 or ZrO.sub.2 dispersed
active metal oxide is prepared through a precipitate deposition
method by taking Cr.sub.2O.sub.3, Al.sub.2O.sub.3 or ZrO.sub.2 as
carriers. Taking preparation of oxide by dispersed ZnO as an
example, commercial Cr.sub.2O.sub.3, Al.sub.2O.sub.3 or ZrO.sub.2
carrier is dispersed in a base solution in advance, and then mixed
and precipitated at room temperature with a sodium hydroxide
precipitant by taking zinc nitrate as raw material. The molar
concentration of Zn.sup.2+ is 0.067M; and the ratio of molar
fractions of Zn.sup.2+ and the precipitant is 1:8; and then aging
is conducted at 160.degree. C. for 24 hours to obtain carrier
Cr.sub.2O.sub.3, Al.sub.2O.sub.3 or ZrO.sub.2 dispersed ZnO oxide
(the contents of the dispersing agents in catalyst A are 0.1 wt %,
10 wt % and 90 wt %).
[0046] The etching process is the same as the preparation processes
of products ZnO 3, ZnO 5 and ZnO 8 in step (2) in above (I). The
catalyst having a great number of surface oxygen vacancies is
synthesized. The surface oxygen vacancies are 65%, 30% and 25%. The
aftertreatment process is the same as step (3) in above (I).
[0047] Corresponding products from top to bottom are defined as
dispersed oxides 1-3. The same method is used to obtain carrier
Cr.sub.2O.sub.3, Al.sub.2O.sub.3 or ZrO.sub.2 dispersed MnO oxide
(the contents of the dispersing agents in catalyst A are 5 wt %, 30
wt % and 60 wt %). The surface oxygen vacancies are 62%, 27% and
28%. Corresponding products from top to bottom are defined as
dispersed oxides 4-6.
[0048] II. Preparation of Catalyst B (Zeolite of CHA and AEI
Topologies):
[0049] The CHA and/or AEI topology has eight-membered ring orifices
and a three-dimensional porous channel and comprises cha cage.
[0050] 1) The specific preparation process is as follows:
[0051] The raw materials of 30% (mass concentration) of silica sol,
AlOOH, phosphoric acid, TEA (R) and deionized water are weighed
according to oxide SiO.sub.2: Al.sub.2O.sub.3: H.sub.3PO.sub.4: R:
H.sub.2O=1.6:16:32:55:150 (mass ratio); after mixing at room
temperature, 0.5 time of molar weight of auxiliary HF is added to a
template agent; carrier oxide powder is added; the mixture is
stirred and aged at 30.degree. C. and then transferred into a
hydrothermal reactor after 2 h, and crystallized at 200.degree. C.
for 24 h. The water bath is quenched to room temperature.
Centrifugal washing is conducted repeatedly so that the pH of the
supernatant is 7 at the end of washing. After the precipitate is
dried at 110.degree. C. for 17 h, the precipitate is calcined in
air at 600.degree. C. for 3 h to obtain the supported
silicon-phosphorus-aluminum inorganic solid acid.
[0052] The skeleton element composition of the zeolite of CHA and
AEI topologies may be one or more than two of Si--O, Si--Al--O,
Si--Al--P--O, Al--P--O, Ga--P--O, Ga--Si--Al--O, Zn--Al--P--O,
Mg--Al--P--O and Co--Al--P--O.
[0053] O element of part of the skeleton is connected with H, and
corresponding products are successively defined as parts 1-7.
TABLE-US-00003 TABLE 3 Preparation of Zeolite of CHA or AEI
Topology and Performance Parameters Sample Aluminum Template Hydro-
Time Number Si Source Source P Source Agent Auxiliary Mass Ratio
thermal (Day) Carrier Molecular part 1 TEOS sodium phosphoric TEA
SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 180 1
Al.sub.2O.sub.3 4 metaaluminate acid 1.6:16:32:55:150 part 2 silica
sol Al(OH).sub.3 phosphoric Mor HCl
SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 150 4
SiO.sub.2 15 acid 2.4:19:30:15:150 part 3 TEOS AlOOH phosphoric
TEAOH HF SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 160
4 TiO.sub.2 28 acid 0.7:15:32:55:150 part 4 silica sol aluminum
phosphoric DIPEA
SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 170 2.5
ZrO.sub.2 34 isopropoxide acid 1.1:17:32:55:150 part 5 aluminum
phosphoric TEAOH HF Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O =
190 1 CeO.sub.2 24 sulfate acid 16:32:55:150 part 6 silica sol
aluminum phosphoric DIPEA
SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 200 1 MgO 8
nitrate acid 0.5:17:32:55:150 part 7 TEOS aluminum phosphoric TEA
HF SiO.sub.2:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 170 0.7
Ga.sub.2O.sub.3 20 sulfate acid 0.3:18:32:55:150 part 8 aluminum
phosphoric TEA HCl Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 160
3.5 Al.sub.2O.sub.3 31 nitrate acid 11:32:55:150 (2) Zeolite
composed of other elements Hydro- thermal Molecular Temper- Sieve
Sample Precursor Precursor Precursor Template ature Time Loading
Number 1 2 3 Agent Auiliary Mass Ratio (.degree. C.) (Day) Carrier
wt % part 9 TEOS TEA HF SiO.sub.2:R:H.sub.2O = 180 1 SiO.sub.2 45
1.6:55:150 part 10 silica sol Al(OH).sub.3 Mor HF
SiO.sub.2:Al.sub.2O.sub.3:R:H.sub.2O = 150 4 Al.sub.2O.sub.3 10
2.4:19:15:150 part 11 gallium phosphoric TEAOH HF
Ga2O3:H.sub.3PO.sub.4:R:H.sub.2O = 160 4 TiO.sub.2 22 nitrate acid
15:32:55:150 part 12 silica sol gallium phosphoric TEA HF
SiO.sub.2:Ga.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 170 2.5
ZrO.sub.2 6 nitrate acid 1.1:17:32:55:150 Part 13 zinc aluminum
phosphoric TEAOH HF ZnO:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O
= 190 1 CeO.sub.2 25 nitrate sulfate acid 0.5:16:32:55:150 part 14
magnesium aluminum phosphoric TEA
MgO:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O = 200 1 MgO 8
nitrate nitrate acid 0.5:17:32:55:150 part 15 gallium aluminum
phosphoric TEA HF Ga2O3:Al.sub.2O.sub.3:H.sub.3PO.sub.4:R:H.sub.2O
= 170 0.7 Ga.sub.2O.sub.3 11 nitrate sulfate acid
0.4:18:32:55:150
[0054] The reference example is part 16; other conditions are the
same as those of part 1; and the zeolite loading is changed to
1%.
[0055] The reference example is part 17; other conditions are the
same as those of part 1; and the zeolite loading is changed to
70%.
[0056] III. Catalyst Preparation
[0057] The catalyst A and the catalyst B in the required ratio are
added to the container to achieve the purposes of separation,
crushing, uniform mixing and the like through one or more than two
of extrusion force, impact force, shear force and friction force
generated by high-speed motion of the material and/or the
container, so as to realize conversion of mechanical energy,
thermal energy and chemical energy by regulating the temperature
and the atmosphere of carrier gas, thereby further enhancing the
interaction between different components.
[0058] In the mechanical mixing process, the mixing temperature can
be set as 20-100.degree. C., and the mechanical mixing process can
be conducted in an atmosphere or directly in the air. The
atmosphere is one or more than one of: a) nitrogen and/or inert
gas; b) mixed gas of hydrogen, nitrogen and/or inert gas, with the
volume ratio of hydrogen in the mixed gas being 5-50%; c) mixed gas
of carbon monoxide, nitrogen and/or inert gas, with the volume
ratio of carbon monoxide in the mixed gas being 5-20%; and d) mixed
gas of oxygen, nitrogen and/or inert gas, with the volume ratio of
oxygen in the mixed gas being 5-20%. The inert gas is one or more
than one of helium, argon and neon.
[0059] Mechanical stirring: mixing the catalyst A and the catalyst
B with a stirring rod in a stirring tank; and regulating the mixing
degree and the relative distance of the catalyst A and the catalyst
B by controlling stirring time (5 min-120 min) and rate (30-300
r/min).
[0060] Ball milling: Rolling at high speed in a grinding tank by
using abrasive and the catalysts; and producing strong impact and
milling on the catalysts to achieve the effects of dispersing and
mixing the catalyst A and the catalyst B. The ratio of the abrasive
(which is stainless steel, agate and quartz; and the size range is
5 mm-15 mm) to the catalysts (the mass ratio scope is 20-100:1) is
controlled to regulate the particle size and the relative distance
of the catalysts.
[0061] Shaking table mixing: premixing the catalyst A and the
catalyst B and placing the catalysts into the container; realizing
the mixing of the catalyst A and the catalyst B by controlling the
reciprocating oscillation or circumferential oscillation of a
shaking table; and realizing uniform mixing and regulating the
relative distance by regulating oscillation speed (range: 1-70
r/min) and time (range: 5 min-120 min).
[0062] Mechanical grinding: premixing the catalyst A and the
catalyst B and placing the catalysts into the container; and under
certain pressure (range: 5 kg-20 kg), making relative motion (speed
range: 30-300 r/min) by the ground and mixed catalysts to achieve
the effects of regulating the particle size and the relative
distance of the catalysts and realizing uniform mixing.
[0063] Specific catalyst preparation and parameter features are
shown in Table 6.
TABLE-US-00004 TABLE 6 Preparation of Catalysts and Parameter
Features Compounding Mode and Condition Mechanical Ball Milling
Mechanical Agitation Abrasive Rocking Bed Polishing Rate Material,
Oscillation Pressure (kg) Catalyst Catalyst Weight (r/min) Size
Range and Speed and Relative Geometrical Catalyst Component
Component Ratio and Time Catalyst Mass (r/min) Movement Center
Distance Number A B of A to B (min) Ratio and Time Rate (r/min) of
A and B Particles A ZnO1 part 1 0.33 170, 60 50 .mu.m B ZnO 2 part
2 0.5 10, 50 3 mm C ZnO3 part 3 2 5 mm stainless 502 .mu.m steel
ball, 30:1 D ZnO4 part 4 1 6 mm stainless 80 nm steel ball, 600:1 E
ZnO 5 part 5 1 5, 10 1 mm F ZnO 6 part 6 3 60, 100 600 .mu.m G ZnO7
part 7 3 50, 30 300 nm H ZnO8 part 8 1 100, 300 400 nm I spinel 1
part 9 5 6 mm agate 40 .mu.m ball, 110:1 J spinel 2 part 10 1 70,
100 500 .mu.m K spinel 3 part 11 3 5, 20 2.5 mm L spinel 4 part 12
0.33 2, 30 4 mm M spinel 5 Part 13 1 10, 10 2 mm N spinel 6 part 14
3 6 mm quartz, 10:1 1.5 mm O spinel 7 part 15 0.33 6 mm quartz,
10:1 1.5 mm P MnO 1 part 1 1 1, 10 2.5 mm Q MnO 2 part 2 1 200, 250
700 .mu.m R MnO 3 part 3 3 5 mm stainless 50 .mu.m steel ball, 50:1
S CeO1 part 4 1 10, 100 100 .mu.m T CeO2 part 5 4 50, 600 300 .mu.m
U CeO3 part 6 3 10, 100 100 .mu.m V dispersed part 7 20 5 mm
stainless 3 mm oxide 1 steel ball, 10:1 W dispersed part 8 0.5 5,
30 3 mm oxide 2 X dispersed part 9 1 100, 250 500 .mu.m oxide 3 Y
dispersed part 10 3 5 mm stainless 100 nm oxide 4 steel ball, 200:1
Z dispersed part 11 1.5 6 mm stainless 8 .mu.m oxide 5 steel ball,
60:1 Z1 dispersed part 12 2.5 70, 100 300 .mu.m oxide 6 Z2 MnO 1
Part 13 1.5 60, 100 600 .mu.m Z3 ZnO 1 part 14 2 50, 30 300 nm Z4
dispersed part 15 10 100, 200 400 .mu.m oxide 1 Z5 spinel 1 part 1
0.1 20, 100 500 .mu.m Z6 ZnO1 part 1 1 20, 300 100 .mu.m Z7 MnO 1
part 1 1.5 60, 10 1 mm Z8 dispersed part 1 4 5 mm stainless 15
.mu.m oxide 1 steel ball, 50:1 Z9 spinel 1 part 1 4.5 100, 120 500
nm Z10 dispersed part 1 2.5 100, 200 400 nm oxide 1 Z11 spinel 1
part 1 3 20, 200 150 .mu.m Comparison 1 ZnO 9 part 1 3 20, 30 1 mm
Comparison 2 Zn 10 part 1 2 60, 100 1 mm
[0064] Example of Catalytic Reactions
[0065] A fixed bed reaction is taken as an example, but the
catalyst is also applicable to a fluidized bed reactor. The
apparatus is equipped with gas mass flow meters and online product
analysis chromatography (the tail gas of the reactor is directly
connected with the metering valve of chromatography, and thus
periodic and real-time sampling and analysis will be achieved).
[0066] 2 g of the above catalyst in the present invention is placed
in a fixed bed reactor. The air in the reactor is replaced with Ar;
and then the temperature is raised to 300.degree. C. in the H.sub.2
atmosphere, and then the syngas (H.sub.2/CO molar ratio=0.2-3.5) is
switched. The pressure of the syngas is 0.5-10 MPa. The temperature
is raised to reaction temperature of 300-600.degree. C., and the
air velocity of the reaction raw gas is regulated to 500-1000
ml/g/h. On-line chromatography is used to detect and analyze the
product.
[0067] The reaction performance can be changed by changing the
temperature, pressure, space velocity and H.sub.2/CO molar ratio in
the syngas. The sum of selectivity of the light olefins, the
ethylene, the propylene and the butylene is 50-90%. Due to the low
hydrogenation activity of the surface of the metal composite of the
catalyst, a large amount of methane will not be avoided and the
selectivity of the methane is low.
TABLE-US-00005 TABLE 7 Specific Application and Effect Data of
Catalysts GHSV Temperature H.sub.2/CO Pressure CO Light CH.sub.4
Alkene/ Embodiment Catalyst (h.sup.-1) (.degree. C.) Molar Ratio
(MPa) Conversion olefins Selectivity % Alkane Ratio 1 A 8000 410 2
3.5 19.9 81.6 5.5 10.2 2 B 3000 400 5.5 0.9 33.6 80.3 5.6 10.0 3 C
8000 380 3 4.5 27.5 89.5 2.5 14.8 4 D 3000 370 6 10 29.4 68.8 13.5
5.3 5 E 10000 470 3.5 1.5 24.6 75.3 3.3 6.3 6 F 2000 400 4.5 7 51.3
81.9 2.6 8.2 7 G 3000 380 6.5 2.5 34.7 73.9 11.7 10.6 8 H 500 370
8.5 5 33.5 69.9 10.8 7.0 9 I 2300 370 1 3.5 26.6 79.6 6.1 11.4 10 J
4000 410 2.5 5 35.6 88.7 2.7 17.7 11 K 1000 430 2.5 3 56.9. 80.9
4.8 11.6 12 L 9500 520 1 4 14.6 85.9 8.1 14.3 13 M 600 480 0.5 9
15.3 65.7 12.5 4.4 14 N 9100 470 3 6 34.8 85.3 2.5 12.2 15 O 8200
450 1.5 5 33.9 84.7 2.9 14.1 16 P 8000 450 2.5 5 30.4 86.9 2.7 14.5
17 Q 600 350 3.5 5 25.6 73.8 3.5 6.2 18 R 2100 350 6 7 17.9 80.8
6.3 11.5 19 S 2500 400 4 6 55.7 77.7 6.1 11.1 20 T 4000 400 4 4
32.5 72.1 10.5 9.0 21 U 3500 400 4 3 24.9 74.0 9.7 6.2 22 V 8600
450 2.5 4 26.3 83.5 2.9 11.9 23 W 5500 410 0.3 3.5 15.8 84.6 3.7
14.1 24 X 3000 400 5.5 0.9 15.8 77.1 5.9 7.7 25 Y 2000 360 7 2.5
37.1 64.7 13.5 4.3 26 Z 800 370 5 10 40.3 71.9 11.6 5.1 27 Z 1
10000 470 1.5 1.5 19.8 77.4 12.3 15.5 28 Z 2 4000 400 3.5 7 48.6
87.5 3.7 17.5 29 Z 3 3000 380 5.5 2.5 20.4 68.8 10.7 6.9 30 Z 4
2000 400 4 3.5 15.3 51.6 11.7 2.9 31 Z5 2500 400 4.5 10 17.7 53.7
3.9 2.8 32 Z6 2000 350 3 4 15.8 78.3 2.8 6.5 33 Z7 4500 400 2.5 3
46.6 85.7 3.1 9.5 34 Z8 4000 400 3 4 53.9 86.0 3.5 12.3 35 Z9 2000
350 2.5 3 27.9 70.3 8.8 6.4 36 Z10 1500 350 3 4 31.4 68.9 9.6 5.7
37 Z11 4200 400 2.5 4 34.4 77.2 3.5 6.4 38 C 4000 380 3 4.5 51.3
80.1 3.5 8.0 39 J 2000 410 2.5 5 52.9 81.4 2.4 8.1 40 Reference
3000 320 0.5 1 1.1 30.3 35.5 2.5 example 1 41 Reference 2000 350 1
2 18.7 37.5 45.9 2.5 example 2 42 Reference 4000 450 3 3 28.1 28.3
27.1 1.8 example 3 43 Reference 2000 350 2.5 3 0.3 27.3 61.7 1.6
example 4 44 Reference 2000 410 1.5 3 24.6 46.2 9.7 1.5 example 5
45 Reference 3000 400 2 3.5 31.2 19.5 10.8 0.9 example 6 46
Reference 8000 410 2 3.5 10.3 46.1 37.9 1.8 example 7 47 Reference
8000 410 2 3.5 52.1 43.7 28.1 1.7 example 8 48 Reference 8000 380 3
4.5 7.2 65.5 17.5 4.7 example 9 49 Reference 4000 380 3 4.5 13.6
48.1 15.5 1.6 example 9 50 Reference 8000 380 3 4.5 38.4 49.5 2.5
1.3 Example 10 51 Reference 4000 380 3 4.5 52.5 37.1 3.5 0.7
Example 10
[0068] In reference example 1, the catalyst component A is ZnO 9,
and component B is part 1.
[0069] In reference example 2, the catalyst component A is Zn 10,
and component B is part 1.
[0070] The component A in the catalyst adopted in reference example
3 is metal ZnCo+ part 1. The molar ratio of ZnCo is 1:1. The mass
ratio of ZnCo to part 1 is 1:1. Other parameters and the mixing
process are the same as those of catalyst C.
[0071] The catalyst adopted in reference example 4 is metal
TiO.sub.2+ part 1 without surface oxygen vacancy. Other parameters
and the mixing process are the same as those of catalyst C.
[0072] The zeolite in the catalyst adopted in reference example 5
is a commodity SAPO-34 purchased from Nankai University Catalyst
Factory without carrier dispersion.
[0073] The zeolite in the catalyst adopted in reference example 6
is a commodity ZSM-5 purchased from Nankai University Catalyst
Factory, wherein the zeolite is of a full microporous structure,
and the silica alumina ratio is 30, without carrier dispersion.
[0074] Reaction results of reference examples 5 and 6 show that,
the topology and the carrier dispersion of CHA or AEI are crucial
to the selective modulation of the products.
[0075] The distance between the metal oxide and the zeolite in the
catalyst adopted in reference example 7 is 10 mm. Other parameters
and the mixing process are the same as those of catalyst C.
[0076] The metal oxide in the catalyst adopted in reference example
8 is located in porous channels of the zeolite and is in close
contact with the porous channels. Other parameters and the like are
the same as those of catalyst C.
[0077] Results of reference examples 7 and 8 show that, the
distance between component A and component B is also crucial to
product selectivity.
[0078] In the reference technology of the document (Jiao et al.,
Science 351 (2016) 1065-1068), the SAPO-34 zeolite contained no
carrier. When the conversion rate is 17, alkene selectivity is 80%,
but the space velocity is reduced. When the conversion rate is
increased to 35%, alkene selectivity is 69%, alkane selectivity is
20%, and alkene/alkane ratio is decreased to 3.5.
[0079] For the catalysts in the reference examples 9 and 10, other
conditions are the same as those of C; and only the zeolites are
respectively replaced with part 16 and part 17.
[0080] It can be seen from the reference example 9 that, the
zeolite loading is too low, which results in slightly high
selectivity of methane and slightly low selectivity of alkene.
[0081] It can be seen from the reference example 10 that, the
zeolite loading is too high, which results in excessive
hydrogenation and slightly low selectivity of alkene. Especially
after the space velocity is reduced and the conversion rate is
increased, compared with the catalyst C, the alkene/alkane ratio is
obviously reduced.
[0082] It is observed that from the above table that, the structure
of the zeolite including the topologies, acid strength and acid
amount of CHA&AEI, and the matching of the distance between the
metal oxide and the zeolite are crucial and directly affect the
conversion rate of carbon monoxide and propylene and butylene
selectivity.
* * * * *